CN108728155A - A kind of double solvents and its application - Google Patents
A kind of double solvents and its application Download PDFInfo
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- CN108728155A CN108728155A CN201710240800.4A CN201710240800A CN108728155A CN 108728155 A CN108728155 A CN 108728155A CN 201710240800 A CN201710240800 A CN 201710240800A CN 108728155 A CN108728155 A CN 108728155A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/08—Azeotropic or extractive distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
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- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to Aromatics Extractive Project fields, disclose a kind of double solvents and its application, the double solvents includes main solvent, cosolvent and olefinic polymerization inhibitor, on the basis of the total weight of double solvents, the content of the main solvent is 70-99 weight %, the content of the cosolvent is 0.999-29.9 weight %, and the content of the olefinic polymerization inhibitor is 10-1000 μ g/g；The main solvent is selected from sulfone compound；The cosolvent is selected from least one of N-Methyl pyrrolidone, triethylene glycol monomethyl ether, tetraethylene glycol monomethyl ether, furfural and dimethylacetylamide；The olefinic polymerization inhibitor is selected from least one of p-tert-Butylcatechol, diethyl hydroxylamine, dipropyl azanol, 2- sec-butyl -4,6- dinitrophenol and sodium nitrite.The double solvents has aromatic hydrocarbons and sulfide highly selective, reduces the selectivity to alkene, and inhibit the polymerization of alkene, is highly suitable for applying in extractive distillation.
Description
Technical field
The present invention relates to Aromatics Extractive Project fields, and in particular, to a kind of double solvents and its application.
Background technology
Aromatics Extractive Project is the process for detaching high purity aromatics from hydrocarbon mixture by the effect of selective solvent.It extracted
The technical indicator of journey depends greatly on the performance of solvent.One good industrial extraction solvent should have following characteristic：
The selectivity of aromatic hydrocarbons will be got well, the purity for improving aromatic hydrocarbons is conducive to；It is big to aromatic hydrocarbons solvability, in favor of reducing solvent ratio and behaviour
Make expense；It is big with the boiling-point difference of aromatic hydrocarbons, to be detached with solvent；Thermal stability and chemical stability are good, with ensure aromatic hydrocarbons not by
Degradation material is polluted；Nontoxic, non-corrosive, easy to operation and equipment material is chosen；It is cheap and easy to get.
The double solvents that CN1393507A proposes a kind of method of extractive distillation aromatics separation and uses, double solvents packet
Include main solvent and cosolvent and modifying agent.Any one or two kinds of the cosolvent in C8-C1l aromatic hydrocarbons have not
With the mixture of carbon number aromatic hydrocarbons solvent recovery operation item can be significantly mitigated when the double solvents is for extractive distillation recycling aromatic hydrocarbons
Part improves aromatic recovery rate, and the aromatic hydrocarbons that may make is in neutrality.But the selectivity of the cosolvent itself is still not ideal enough, boiling
Point is relatively low, and generally 140-200 DEG C, waste when for C6-C7 fraction extractive distillation aromatics separations is larger, to boiling point model
It encloses not applicable compared with the extractive distillation of long distillate.
CN1393507A discloses the double solvents used in a kind of separation of extractive distillation aromatic hydrocarbons, including 68-98.8 mass %
The water of main solvent, the cosolvent of 1-30 mass % and 0.2-2.0 mass %, the main solvent are selected from sulfone compound, glycol
Class compound, N- formoxyls beautiful jade or N-Methyl pyrrolidone, cosolvent be selected from tool there are two phenyl ring hydrocarbon compound, two
Phenyl ring is interconnected to form condensed ring or is connected by single chemical bond.It is added in conventional extracting rectifying selective solvent
Compound on a small quantity containing two phenyl ring is cosolvent, significantly enhances solvability of the solvent to aromatic hydrocarbons.But there are two benzene for tool
The introducing of the hydrocarbon compound of ring brings difficulty to the separation of solvent and aromatic hydrocarbons, increases energy consumption.
Therefore, there is an urgent need for develop a kind of highly efficient double solvents so that double solvents is more preferable to the selectivity of aromatic hydrocarbons, more
It is easy to and aromatics seperation.
Invention content
The purpose of the present invention is overcoming prior art aromatic hydrocarbon extraction solvent poor to arenes selectivity, and solvent and aromatic hydrocarbons are not easy
In the defect of separation, a kind of double solvents and the application of the double solvents are provided.
In addition, as people are to the pay attention to day by day of environmental protection, environmental regulation is also increasingly stringent, and the sulphur for reducing gasoline contains
Amount is considered as improving one of the most important measure of air quality.Most of sulphur in China's gasoline products come from hot-working vapour
Oily blending component, such as catalytically cracked gasoline.Therefore, it is necessary to which catalytically cracked gasoline is carried out deep desulfuration, simple catalytic gasoline
Desulfurization technology can all bring a problem：The octane number of catalytic gasoline declines.
The present inventor has found in the course of the research, and gasoline to be desulfurization is cut, and then evaporates middle gasoline
Divide and carry out Aromatics Extractive Project distillation processing, uses double solvents that can so that aromatic hydrocarbons and sulfide are dissolved in compound molten in middle gasoline fraction
Dosage form effectively separates sulfide and olefin component at rich solvent, partly avoids in sweetening process, caused by the saturation of alkene
The rich solvent is further carried out stripping processing by loss of octane number, can be separated solvent, sulfur-rich aromatic hydrocarbons, sulfur-rich aromatic hydrocarbons
Selective hydrodesulfurization device can be entered and carry out desulfurization process.The present inventor further study show that, in main solvent
Addition is selected from N-Methyl pyrrolidone, triethylene glycol monomethyl ether, tetraethylene glycol monomethyl ether, furfural and dimethyl simultaneously in sulfone compound
The cosolvent of at least one of acetamide and selected from p-tert-Butylcatechol, diethyl hydroxylamine, dipropyl azanol, 2- Zhong Ding
The olefinic polymerization inhibitor of at least one of base -4,6- dinitrophenol and sodium nitrite, can not only ensure double solvents
To the selectivity of aromatic hydrocarbons and sulfide, while the selectivity to alkene is reduced, efficiently separates out aromatic hydrocarbons, and molten rich in aromatic hydrocarbons
Agent is easily isolated, and can effectively inhibit the polymerization of alkene using a small amount of olefinic polymerization inhibitor.In the preferred case, by N- methyl
Pyrrolidones and triethylene glycol monomethyl ether and/or tetraethylene glycol monomethyl ether with the use of be more advantageous to improve double solvents to aromatic hydrocarbons and
The selectivity of sulfide reduces the selectivity to alkene, in the case that further preferably, is added in main solvent, cosolvent slow
Erosion agent can ensure long-term operation of the main solvent under complicated material condition.
Based on this, the present invention provides a kind of double solvents, which includes main solvent, cosolvent and olefinic polymerization suppression
Preparation, on the basis of the total weight of double solvents, the content of the main solvent is 70-99 weight %, the content of the cosolvent
Content for 0.999-29.9 weight %, the olefinic polymerization inhibitor is 10-1000 μ g/g；
The main solvent is selected from sulfone compound；
The cosolvent is selected from N-Methyl pyrrolidone, triethylene glycol monomethyl ether, tetraethylene glycol monomethyl ether, furfural and dimethyl second
At least one of amide；
The olefinic polymerization inhibitor is selected from p-tert-Butylcatechol, diethyl hydroxylamine, dipropyl azanol, 2- Zhong Ding
At least one of base -4,6- dinitrophenol and sodium nitrite.
The present invention also provides application of the double solvents in extractive distillation.
Double solvents provided by the invention has the following advantages that compared with existing double solvents：
(1) double solvents provided by the invention has higher dissolubility and selectivity；
(2) double solvents provided by the invention can handle the broader raw material of boiling spread；
(3) while double solvents provided by the invention can ensure the selectivity to sulfide, the choosing to alkene is reduced
Selecting property；
(4) when also containing corrosion inhibiter in double solvents, it can ensure that long period fortune of the main solvent under complicated material condition
Row.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Specific implementation mode
The specific implementation mode of the present invention is described in detail below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or
Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively
It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more
New numberical range, these numberical ranges should be considered as specific open herein.
The present invention provides a kind of double solvents, which includes main solvent, cosolvent and olefinic polymerization inhibitor, with
On the basis of the total weight of double solvents, the content of the main solvent is 70-99 weight %, and the content of the cosolvent is 0.999-
The content of 29.9 weight %, the olefinic polymerization inhibitor are 10-1000 μ g/g；
The main solvent is selected from sulfone compound；
The cosolvent is selected from N-Methyl pyrrolidone, triethylene glycol monomethyl ether, tetraethylene glycol monomethyl ether, furfural and dimethyl second
At least one of amide；
The olefinic polymerization inhibitor is selected from p-tert-Butylcatechol, diethyl hydroxylamine, dipropyl azanol, 2- Zhong Ding
At least one of base -4,6- dinitrophenol and sodium nitrite.
The present inventor has found sulfone compound as main solvent in the course of the research, and cooperation is of the present invention to be helped
Solvent and olefinic polymerization inhibitor can not only improve solvent to arenes selectivity, also overcome solvent and aromatic hydrocarbons is not easy to point
From defect.In addition, main solvent, cosolvent and olefinic polymerization inhibitor are used in conjunction with, one-component function will not be caused
Subside.It should be noted that double solvents provided by the invention enables to Aromatic Hydrocarbon in Gasoline to be desulfurization and sulfide to be dissolved in
Double solvents forms rich solvent, effectively separates sulfide and olefin component, partly avoids in sweetening process, the saturation of alkene
Caused by loss of octane number.Double solvents provided by the invention is compared with existing double solvents, is ensureing the selection to sulfide
Property while, reduce to the selectivity of alkene.
In order to further increase selectivity of the double solvents to aromatic hydrocarbons and sulfide, the selectivity to alkene is reduced, preferably
Ground, on the basis of the total weight of double solvents, the content of the main solvent is 80-95 weight %, and the content of the cosolvent is
The content of 4.99-19.9 weight %, the olefinic polymerization inhibitor are 100-1000 μ g/g, it is further preferred that with compound molten
On the basis of the total weight of agent, the content of the main solvent is 85-90 weight %, and the content of the cosolvent is 9.95-14.9 weights
% is measured, the content of the olefinic polymerization inhibitor is 500-1000 μ g/g.
According to the present invention, the content of olefinic polymerization inhibitor refers to that, relative to every g double solvents, olefinic polymerization inhibits
The amount of agent.
In double solvents provided by the present invention preferably do not contain water, but absolutely exclude water there are situations, when described
When containing water in double solvents, preferably in terms of the total amount of double solvents, the content of water is not more than 3 weight %.
A preferred embodiment of the invention, the cosolvent are N-Methyl pyrrolidone and triethylene glycol monomethyl ether
And/or the mixture of tetraethylene glycol monomethyl ether.Main solvent is more advantageous to using this kind of preferred embodiment and cosolvent collaboration plays
Effect further decreases the selectivity to alkene while ensureing the selectivity to sulfide.
In the present invention, it is preferred in terms of the N-Methyl pyrrolidone of 100 parts by weight, the triethylene glycol monomethyl ether and/or
The dosage of tetraethylene glycol monomethyl ether is 10-200 parts by weight, further preferably 50-100 parts by weight.Using this kind of preferred implementation side
Formula is more advantageous to the effect for playing N-Methyl pyrrolidone and triethylene glycol monomethyl ether and/or tetraethylene glycol monomethyl ether, is ensureing to sulphur
While the selectivity of compound, the selectivity to alkene is further reduced, while but also double solvents can handle boiling point model
Enclose broader raw material.
It should be noted that when the cosolvent is sweet containing N-Methyl pyrrolidone and triethylene glycol monomethyl ether and four simultaneously
When alcohol monomethyl ether, the dosage of the triethylene glycol monomethyl ether and/or tetraethylene glycol monomethyl ether refers to triethylene glycol monomethyl ether and tetraethylene glycol
Total dosage of monomethyl ether.
A preferred embodiment of the invention, the olefinic polymerization inhibitor be tert-butyl catechol and/or
2- sec-butyl -4,6- dinitrophenol, the preferred olefinic polymerization inhibitor in double solvents main solvent and cosolvent match
It closes in use, having the function of preferably inhibiting olefinic polymerization, double solvents performance more excellent.
The present invention is wider to the range of choice of the sulfone compound, can be various sulfone class chemical combination commonly used in the art
Object, such as the sulfone compound can be in sulfolane, 3- methyl sulfolanes, dimethyl sulfone and diη-propyl sulfones at least
One kind, preferably sulfolane.Solubility of the sulfolane in hydrocarbon is preferable, more excellent to the selectivity of aromatic hydrocarbons.
Double solvents based on sulfone compound in the process of running, due to O in system2Be mixed into, easily aoxidize
Effect generates acid compound and acidic polymer shows sulfone class chemical combination when the pH value in system drops to 4.5 or less
Object degrading solvent, such case can generate equipment certain corrosion, for control system acidity so that the pH value in system is kept
6.0 or so, the preferably described double solvents further includes corrosion inhibiter.
There is no particular limitation to the corrosion inhibiter by the present invention, as long as energy control system is acid, while ensuring the slow of addition
Erosion agent does not influence the performance of double solvents, it is preferable that the corrosion inhibiter is selected from monoethanolamine, diethanol amine, N- methyl lists
At least one of ethanol amine and N methyldiethanol amine, most preferably monoethanolamine.
In the present invention, it is preferable that other substance migrations in the corrosion inhibiter cooperation double solvents, it can effective control system
Acidity, so that it is guaranteed that the acid stable of whole system, also functions to the effect for inhibiting olefinic polymerization to a certain extent.
The present invention is wider to the range of choice of the dosage of the corrosion inhibiter, it is preferable that using the total weight of double solvents as base
The content of standard, the corrosion inhibiter is 10-1000 μ g/g, and further preferably 100-1000 μ g/g are still more preferably 500-
1000μg/g。
The present invention also provides application of the above-mentioned double solvents in extractive distillation.
Double solvents provided by the present invention is suitable for extractive distillation technical process, is steamed suitable for the Aromatics Extractive Project of plurality of raw materials
Evaporate, for example, the gasoline fraction of Hydrocracking technique, reformed oil, coal tar, especially suitable for boiling range be 40-170 DEG C (into
The preferred boiling range of one step be 60-125 DEG C) middle gasoline fraction.
The method that distillation is stripped using double solvents provided by the invention can be according to the arbitrary side of this field routine
Method carries out, including but not limited to：Double solvents is introduced into extraction distillation tower, the middle gasoline fraction that boiling range is 40-170 DEG C from top
Introduce in the middle part of the extraction distillation tower, by extractive distillation, raffinate oil (the non-sulfur material of non-aromatics) be discharged from extractive distillation top of tower,
Enter return tank after condensed, cooling, a portion passes back into extraction distillation tower, and another part transmitting system is subsequently located
Reason；The tapped oil (rich in aromatic hydrocarbons and sulfide) of bottom of tower discharge is detached into stripper, solvent is obtained, contains sulfide
With the product of aromatic hydrocarbons, selective hydrogenation processing is carried out containing the product of sulfide and aromatic hydrocarbons by described, obtained solvent cycle makes
With.
The present invention is not particularly limited the condition of the extractive distillation, and those skilled in the art can be according to handled
Raw material make appropriate choice, such as the condition of extractive distillation may include：It is 60-100 DEG C to enter tower temperature degree, preferably 80-
90℃；Tower top temperature is 70-90 DEG C, preferably 75-85 DEG C；Column bottom temperature is 140-180 DEG C, preferably 155-170 DEG C；Tower top
Pressure (absolute pressure) is 0.05-0.1MPa, and oil ratio (double solvents and raw material weight ratio) is 2-3.
The present invention is not particularly limited the steam stripped condition, those skilled in the art can according to actual conditions into
Row selection appropriate, such as steam stripped condition may include：Tower top temperature is 80-90 DEG C, and column bottom temperature is 170-178 DEG C；Tower
Pressure on top surface is -40 to -60KPa, and reflux/charge-mass ratio is 0.5-1:1.
Below by way of the specific embodiment implementation process that the present invention will be described in detail and generated advantageous effect, it is intended to help
Where reader more clearly understands the Spirit Essence of the present invention, but any restriction cannot be constituted to the practical range of the present invention.
In following embodiment, extractive distillation raw material uses boiling range for 60-125 DEG C of middle gasoline fraction, and the middle gasoline evaporates
It point cuts to obtain by catalytically cracked gasoline, the middle gasoline fraction that boiling range is 60-125 DEG C is at being shown in Table 1.
Gasoline fraction forms in table 1
Embodiment 1
Middle gasoline fraction is introduced in the middle part of extraction distillation tower, double solvents F-1 (concrete composition is shown in Table 2) is introduced from top
(mass ratio of double solvents and middle gasoline fraction is 2 to extraction distillation tower:1), by extractive distillation, extractive distillation condition includes：
It is 84 DEG C to enter tower temperature degree, and tower top temperature is 76-77 DEG C, and column bottom temperature is 158-160 DEG C, and tower top operating pressure is 0.1MPa, is taken out
It proposes overhead discharge to raffinate oil, the tapped oil rich in aromatic hydrocarbons and sulfide of extraction distillation tower bottom of tower enters stripper progress
Stripping, actual conditions include：Tower top temperature is 80-82 DEG C, and column bottom temperature is 177-179 DEG C, and reflux/charge-mass ratio is 1.Tower
Bottom obtains lean solvent, and tower top is obtained containing sulfur-rich aromatic hydrocarbons.It raffinates oil and is listed in table 3 with the analysis result of sulfur-rich aromatic hydrocarbons.System operation 6
After a month, obtained lean solvent pH value is about 7, and without olefin polymerization suspended matter in lean solvent.
2 double solvents of table forms
Note：Double solvents surplus is water
Table 3 raffinates oil, the analysis result of the product of sulfur-rich aromatic hydrocarbons
By calculate it is found that only existed in raffinating oil 3.3 weight % aromatic hydrocarbons (computational methods be (0.1% ×
91.7%)/(0.1% × 91.7%+32.6% × 8.3%) × 100%), the sulphur of 3 weight %, and there are 94.4 weight %
Alkene；There are the aromatic hydrocarbons of 96.7 weight %, the sulphur of 97 weight %, the alkene of 5.6 weight % in sulfur-rich aromatic hydrocarbons.The present invention carries
The double solvents of confession is strong to sulfide and alkene dissolubility, high selectivity, by adding a small amount of olefinic polymerization inhibitor
It is effectively prevent the polymerization of alkene, and can ensure that the long-time of solvent uses by adding a small amount of corrosion inhibiter.
Embodiment 2
It is carried out according to method described in embodiment 1, unlike, using the double solvents F- of the different compositions of phase homogenous quantities
2 alternative composite solvent F-1.Double solvents F-2 compositions are shown in Table 2.After system operation 6 months, obtained lean solvent pH value is about 7,
And without olefin polymerization suspended matter in lean solvent.The aromatic hydrocarbons of 3.5 weight %, the sulphur of 3.2 weight % are only existed in raffinating oil, and are deposited
In the alkene for having 94.9 weight %；There are the aromatic hydrocarbons of 96.5 weight %, the sulphur of 96.8 weight %, 5.1 weights in sulfur-rich aromatic hydrocarbons
Measure the alkene of %.
Embodiment 3
It is carried out according to method described in embodiment 1, unlike, using the double solvents F- of the different compositions of phase homogenous quantities
3 alternative composite solvent F-1.Double solvents F-3 compositions are shown in Table 2.After system operation 6 months, obtained lean solvent pH value is about 7,
And without olefin polymerization suspended matter in lean solvent.Only exist the aromatic hydrocarbons of 3 weight % in raffinating oil, the sulphur of 3 weight %, and there are
The alkene of 93.6 weight %；There are the aromatic hydrocarbons of 97 weight %, the sulphur of 97 weight %, the alkene of 6.4 weight % in sulfur-rich aromatic hydrocarbons.
Embodiment 4
It is carried out according to method described in embodiment 1, unlike, substitute three using the N-Methyl pyrrolidone of phase homogenous quantities
Glycol monomethyl ether.After system operation 6 months, obtained lean solvent pH value is about 7, and without olefin polymerization suspended matter in lean solvent.
The aromatic hydrocarbons of 4.6 weight %, the sulphur of 5 weight % are only existed in raffinating oil, and there are the alkene of 92.4 weight %；Sulfur-rich aromatic hydrocarbons
In there are the aromatic hydrocarbons of 95.4 weight %, the sulphur of 95 weight %, the alkene of 7.6 weight %.
Embodiment 5
It is carried out according to method described in embodiment 1, unlike, N- first is substituted using the triethylene glycol monomethyl ether of phase homogenous quantities
Base pyrrolidones.After system operation 6 months, obtained lean solvent pH value is about 7, and without olefin polymerization suspended matter in lean solvent.
The aromatic hydrocarbons of 4.8 weight %, the sulphur of 4.3 weight % are only existed in raffinating oil, and there are the alkene of 91.9 weight %；Sulfur-rich virtue
There are the aromatic hydrocarbons of 95.2 weight %, the sulphur of 95.7 weight %, the alkene of 8.1 weight % in hydrocarbon.
Embodiment 6
It is carried out according to method described in embodiment 1, unlike, tertiary butyl is substituted using the diethyl hydroxylamine of phase homogenous quantities
Catechol.After system operation 6 months, obtained lean solvent pH value is about 7, occurs a small amount of olefin polymerization in lean solvent and suspends
Object.The aromatic hydrocarbons of 3.9 weight %, the sulphur of 4 weight % are only existed in raffinating oil, and there are the alkene of 92.9 weight %；It is sulfur-rich
There are the aromatic hydrocarbons of 96.1 weight %, the sulphur of 96 weight %, the alkene of 7.1 weight % in aromatic hydrocarbons.
Embodiment 7
It is carried out according to method described in embodiment 1, unlike, N- crassitudes are substituted using the furfural of phase homogenous quantities
Ketone and triethylene glycol monomethyl ether substitute tert-butyl catechol using the sodium nitrite of phase homogenous quantities.After system operation 6 months, obtain
To lean solvent pH value be about 7, and without olefin polymerization suspended matter in lean solvent.The virtue of 5.4 weight % is only existed in raffinating oil
Hydrocarbon, the sulphur of 6.1 weight %, and there are the alkene of 90.6 weight %；There are the aromatic hydrocarbons of 94.6 weight % in sulfur-rich aromatic hydrocarbons,
The sulphur of 93.9 weight %, the alkene of 9.4 weight %.
Embodiment 8
It is carried out according to method described in embodiment 1, unlike, corrosion inhibiter, corrosion inhibiter are not contained in the double solvents
It is substituted with the sulfolane of phase homogenous quantities.The distribution of sulphur, alkene and aromatic hydrocarbons only has minor change, but system operation obtains after 6 months
Lean solvent pH value drop to 5.5, performance declines.
Comparative example 1
Carried out according to method described in embodiment 1, unlike, the double solvents using described in CN1262264A with
The double solvents that sulfolane is main solvent, ortho-xylene is cosolvent substitutes, on the basis of the total weight of the double solvents, institute
The content for stating sulfolane is 94 weight %, and the content of the ortho-xylene is 6 weight %.There are 21 weight %'s in raffinating oil
Aromatic hydrocarbons, the sulphur of 43 weight %, there are the alkene of 58.7 weight %；There are the aromatic hydrocarbons of 79 weight %, 57 weights in sulfur-rich aromatic hydrocarbons
Measure the sulphur of %, the alkene of 41.3 weight %.
It can be seen from the above using double solvents provided by the invention can to raffinate oil middle aromatic hydrocarbons and
Sulfur content is less, and aromatic hydrocarbons and sulfide are more dissolved in double solvents in raw material, and alkene is less to be dissolved in double solvents, is ensureing
In the case of aromatics yield, effectively sulfide and alkene are separated, can be ensured in subsequent processes, it is full in less alkene
Sulfide is effectively removed in the case of.In addition in the preferred case, can ensure to lead when containing corrosion inhibiter in double solvents
Long-term operation of the solvent under complicated material condition.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail can carry out a variety of simple variants to technical scheme of the present invention within the scope of the technical concept of the present invention, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case of shield, it can be combined by any suitable means.In order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (10)
1. a kind of double solvents, which is characterized in that the double solvents includes main solvent, cosolvent and olefinic polymerization inhibitor, with
On the basis of the total weight of double solvents, the content of the main solvent is 70-99 weight %, and the content of the cosolvent is 0.999-
The content of 29.9 weight %, the olefinic polymerization inhibitor are 10-1000 μ g/g；
The main solvent is selected from sulfone compound；
The cosolvent is selected from N-Methyl pyrrolidone, triethylene glycol monomethyl ether, tetraethylene glycol monomethyl ether, furfural and dimethylacetylamide
At least one of；
The olefinic polymerization inhibitor is selected from p-tert-Butylcatechol, diethyl hydroxylamine, dipropyl azanol, sec-butyl -4 2-,
At least one of 6- dinitrophenol and sodium nitrite.
2. double solvents according to claim 1, wherein the content of the main solvent is 80-95 weight %, the hydrotropy
The content of agent is 4.99-19.9 weight %, and the content of the olefinic polymerization inhibitor is 100-1000 μ g/g,
Preferably, the content of the main solvent is 85-90 weight %, and the content of the cosolvent is 9.95-14.9 weight %, institute
The content for stating olefinic polymerization inhibitor is 500-1000 μ g/g.
3. double solvents according to claim 1, wherein the sulfone compound be selected from sulfolane, 3- methyl sulfolanes,
At least one of dimethyl sulfone and diη-propyl sulfone, preferably sulfolane.
4. according to the double solvents described in any one of claim 1-3, wherein the cosolvent is N-Methyl pyrrolidone
With triethylene glycol monomethyl ether and/or the mixture of tetraethylene glycol monomethyl ether.
5. double solvents according to claim 4, wherein in terms of the N-Methyl pyrrolidone of 100 parts by weight, described three is sweet
The dosage of alcohol monomethyl ether and/or tetraethylene glycol monomethyl ether is 10-200 parts by weight, preferably 50-100 parts by weight.
6. double solvents according to claim 4, wherein the olefinic polymerization inhibitor is p-tert-Butylcatechol
And/or 2- sec-butyl -4,6- dinitrophenol.
7. according to the double solvents described in any one of claim 1-6, wherein the double solvents further includes corrosion inhibiter.
8. double solvents according to claim 7, wherein on the basis of the total weight of double solvents, the corrosion inhibiter
Content is 10-1000 μ g/g, preferably 100-1000 μ g/g, further preferably 500-1000 μ g/g.
9. double solvents according to claim 7 or 8, wherein the corrosion inhibiter is selected from monoethanolamine, diethanol amine, N-
At least one of methyl monoethanolamine and N methyldiethanol amine.
10. application of the double solvents described in any one of claim 1-9 in extractive distillation.
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| CN114106869A (en) * | 2020-09-01 | 2022-03-01 | 中国石油化工股份有限公司 | Method for separating aromatic hydrocarbon and alkane in diesel oil fraction and method for processing high aromatic hydrocarbon diesel oil fraction |
| CN115491222A (en) * | 2022-09-23 | 2022-12-20 | 上海兖矿能源科技研发有限公司 | Composite extracting agent and Fischer-Tropsch synthesis distillate oil separation method using same |
| WO2024060399A1 (en) * | 2022-09-23 | 2024-03-28 | 上海兖矿能源科技研发有限公司 | Separation method for high-temperature fischer-tropsch synthesized light oil |
| WO2024145089A1 (en) * | 2022-12-28 | 2024-07-04 | Uop Llc | Improving aromatics extraction through integration of complementary co-solvents |
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